EP0252356B1 - Procédé et four de vapocraquage d'hydrocarbures destines à la fabrication d'oléfines et de dioléfines - Google Patents

Procédé et four de vapocraquage d'hydrocarbures destines à la fabrication d'oléfines et de dioléfines Download PDF

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Publication number
EP0252356B1
EP0252356B1 EP87108912A EP87108912A EP0252356B1 EP 0252356 B1 EP0252356 B1 EP 0252356B1 EP 87108912 A EP87108912 A EP 87108912A EP 87108912 A EP87108912 A EP 87108912A EP 0252356 B1 EP0252356 B1 EP 0252356B1
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Prior art keywords
cracking
tube
hydrocarbons
outlet
inlet
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EP87108912A
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German (de)
English (en)
French (fr)
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EP0252356A1 (fr
Inventor
André Martens
Serge Bellet
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Naphtachimie SA
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Naphtachimie SA
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Priority claimed from FR8609219A external-priority patent/FR2600667B1/fr
Priority claimed from FR8609221A external-priority patent/FR2600642B1/fr
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/04—Thermal processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins

Definitions

  • the present invention relates to a process for cracking hydrocarbons in the presence of water vapor, intended for manufacturing olefins and diolefins, and in particular ethylene.
  • the present invention also relates to a device consisting of a cracking oven intended for the implementation of this process.
  • hydrocarbons are thus in particular transformed, on the one hand, into a gaseous hydrocarbon fraction comprising in particular olefins containing from 2 to 6 carbon atoms, such as ethylene, propylene and isobutene, and diolefins such as butadiene, and, on the other hand, in a liquid hydrocarbon fraction, called "steam cracking gasoline", comprising hydrocarbons containing from 5 to 12 carbon atoms, as well as undesirable by-products, such as methane.
  • ethylene is formed at a higher temperature than higher olefins containing at least 3 carbon atoms. It is known, moreover, that these higher olefins undergo at high temperatures in the presence of hydrogen, secondary hydrocracking and condensation reactions, favoring the formation of light hydrocarbons and gasoline.
  • the yield of olefins, in particular ethylene, and the yield of diolefins, especially butadiene are determined by the weight ratio of the quantities of olefins or of diolefins. produced at the quantity of hydrocarbons used.
  • steam cracking ovens are generally designed to operate under conditions known as high severity. These conditions are, in particular, such that the mixture of hydrocarbons and water vapor circulates in a relatively short time, generally less than one second, in a cracking tube.
  • the cracking temperature is chosen to be generally as high as possible, but which is limited by the thermal stresses of the oven and the cracking tube.
  • the thermal stresses of the cracking tube mainly related to its skin temperature, depend on the nature of the metal or alloy constituting the cracking tube.
  • the pressure of the mixture circulating in the cracking tube is generally relatively low, in order to limit the development of side reactions.
  • the steam cracking oven also includes a heating device consisting of burners arranged on the hearth and / or on the internal walls of the oven.
  • the thermal power of this heating device is generally distributed homogeneously along the cracking tube, so that the mixture of liquid hydrocarbons and water vapor is subjected to a temperature which increases rapidly in the first part of the tube, then more slowly in the second part of the tube. It is known that under these conditions the ethylene yield of a steam cracking oven of a given size is limited mainly by the thermal stresses of the cracking tube and that significant drawbacks can appear, such as coking phenomena inside of the cracking tube and a premature aging effect of the cracking tube.
  • the cracking tubes may be joined two by two and then form a tube having a proportionally larger cross section.
  • the section of the various tubes increases in the direction of flow of the hydrocarbons to be cracked, which makes it possible to transmit to the hydrocarbons for the same temperature, a greater quantity of heat and thus to improve the distribution of the skin temperature of the cracking tubes.
  • such a device does not significantly increase the yield of ethylene and the weight conversion rate of hydrocarbons.
  • a process and a device has now been found consisting of a hydrocarbon cracking furnace in the presence of water vapor, making it possible to very noticeably increase not only the ethylene cracking yield, but also the weight conversion rate of the hydrocarbons.
  • the method and the device of the invention can also be easily adapted to already existing installations for steam cracking of hydrocarbons.
  • Figure 1 is a schematic illustration of a horizontal steam cracking furnace, comprising a thermal radiation enclosure, also applied as a radiation zone, through which a cracking tube disposed in the form of a coil passes.
  • FIG. 2 is a graph showing the increase in the cracking temperature of the mixture of hydrocarbons and water vapor circulating in a cracking tube from the entry to the exit from the radiation zone of an oven steam cracking as a function of the average residence time of the mixture circulating in this tube.
  • Figures 3 and 4 are three-dimensional graphs representing the distribution of the heat flux inside the thermal radiation enclosure of a horizontal steam cracking oven, distribution obtained respectively according to a heating power of non-homogeneous type, as described according to the present invention, and a heating power of homogeneous type.
  • the method according to the present invention is characterized, first of all, by the evolution of the cracking temperature of the mixture of hydrocarbons and water vapor circulating in the tube.
  • This temperature increases along the cracking tube, between the inlet and the outlet of the radiation zone of the furnace, that is to say in the direction of flow of the mixture.
  • the cracking temperature of the mixture of hydrocarbons and water vapor is at the entry of the radiation region of the oven between 500 ° C and 700 ° C, preferably between 550 ° C and 660 ° VS ; it is at the exit of this zone of between 800 ° C and 880 ° C, preferably between 820 ° C and 860 ° C.
  • the mixture of hydrocarbons and steam is, generally subjected to a preheating before entering the radiation area of the oven, this preheating can be achieved by any known means, in particular in a convection heating area of the oven.
  • the method of the invention is characterized in that the increase in the cracking temperature of the mixture is considerably higher in the first half of the length of the tube, located towards the entrance to the radiation zone of the oven only in the second half of the length of the tube located towards the exit of this area.
  • the cracking temperature of the mixture of hydrocarbons and water vapor, circulating in the tube between the inlet and the outlet of the radiation zone of the furnace, is obtained by an inhomogeneous distribution of the power. applied to the tube.
  • the thermal power applied to the first half of the length of the tube, located towards the entrance to the radiation area of the furnace is 1.5 to 5 times greater, preferably 2 to 4 times greater than that applied to the second half of the length of the tube, located towards the exit of this zone; especially when gaseous hydrocarbons are used in the process. It can be 1.5 to 4 times greater, preferably 2 to 3 times greater than that applied to the second half of the length of the tube, when in the process liquid hydrocarbons are used in particular.
  • thermal power is meant here the quantity of heat supplied per unit of time and per unit of volume of the oven surrounding the cracking tube.
  • the average residence time of the mixture of hydrocarbons and water vapor, circulating in the cracking tube between the inlet and the outlet of the radiation zone of the furnace is generally between 300 and 1800 milliseconds, preferably included between 400 and 1400 milliseconds, especially when using gaseous hydrocarbons. It is generally between 300 and 1000 milliseconds, preferably between 400 and 800 milliseconds, in the case of liquid hydrocarbons.
  • the process of the invention is also characterized by the reaction volume of the cracking tube which is not identical in the first and second half of the length of the tube. More specifically, the reaction volume of the second half of the length of the cracking tube, located towards the exit from the radiation zone, is 1.3 to 4 times greater, preferably 1.5 to 2.5 times greater. to that of the first half of the length of the tube, located towards the entrance of this zone. Furthermore, the reaction volume per unit length of the cracking tube increases continuously or discontinuously from the entry to the exit from the radiation zone of the furnace. In practice, it is preferable to carry out this increase in a discontinuous manner, that is to say in stages along the cracking tube.
  • the process of the invention results in increasing not only the hourly yield and production of ethylene, but also the weight conversion rate of hydrocarbons in an oven having a given size and a cracking tube. having a given skin temperature. This result is also obtained with a significant increase in the maximum cracking capacity of an oven having a determined size.
  • composition of the mixture of hydrocarbons and steam, used in the process according to the invention is such that the weight ratio of the quantity of hydrocarbons to the quantity of steam is between 1 and 10, preferably between 2 and 6.
  • the hydrocarbons used in the mixture with the water vapor can be liquid hydrocarbons chosen from naphtha, consisting of hydrocarbons containing approximately from 5 to 10 carbon atoms, light gasolines consisting of hydrocarbons comprising approximately 5 or 6 carbon atoms, the diesel oil consisting of hydrocarbons containing approximately from 8 to 15 carbon atoms, as well as their mixtures. They can, moreover, be used in admixture with saturated and unsaturated hydrocarbons containing from 3 to 6 carbon atoms. They can also be gaseous hydrocarbons constituted by alkanes containing from 2 to 4 carbon atoms, or by their mixtures.
  • alkanes can optionally be used in admixture with alkenes comprising from 2 to 6 carbon and / or methane atoms and / or alkanes comprising 5 or 6 carbon atoms. It is possible, in particular, to use in the process of the invention natural gas, liquefied petroleum gas, also called LPG, or ethane, a secondary product resulting from the steam cracking of liquid hydrocarbons such as naphtha or diesel.
  • LPG liquefied petroleum gas
  • ethane a secondary product resulting from the steam cracking of liquid hydrocarbons such as naphtha or diesel.
  • the steam cracking oven comprises a thermal radiation enclosure through which at least one cracking tube, which is provided in the form of a horizontal or vertical coil, passes.
  • the mean internal diameter and the length of the tube must remain within ranges of values compatible with the mechanical and thermal stresses to which the materials constituting the cracking tube are subjected.
  • the mean internal diameter of the cracking tube is between 70 mm and 160 mm, preferably between 80 mm and 150 mm.
  • the steam cracking oven according to the present invention comprises a cracking tube whose internal diameter increases continuously or discontinuously between the entry and the exit of the thermal radiation enclosure, that is to say in the direction of flow of the mixture of hydrocarbons and water vapor.
  • the increase in the internal diameter of the cracking tube is such that the ratio between the internal diameters of the tube at the outlet and at the inlet of the thermal radiation enclosure is between 1.3 and 3, preferably between 1.6 and 2.2.
  • the internal diameter of the cracking tube at the inlet of the thermal radiation enclosure is preferably between 60 and 90 mm, and that at the outlet of this enclosure is preferably between 110 and 200 mm.
  • the increase in diameter can be continuous all along the cracking tube.
  • a cracking tube made up of a succession of tubes of increasing internal diameter from the inlet to the outlet of the thermal radiation enclosure of the furnace.
  • the increase in the internal diameter of the cracking tube is, in particular, such that the reaction volume of the second half of the length of the tube, located towards the exit from the radiation zone, is 1.3 to 4 times greater, preferably 1.5 to 2.5 times greater than that of the first half of the length of the tube, located towards the entrance to this area.
  • the cracking tube is arranged in the form of a coil made up of a succession of straight sections connected to each other by elbows, these straight sections having increasing internal diameters from the inlet to the outlet of the pipe. thermal radiation enclosure.
  • a variant may consist in using a cracking tube which, after entering the thermal radiation chamber of the furnace, is divided into a bundle of parallel tubes whose internal diameter can be constant, and whose number increases since the entry to the exit of the thermal enclosure, so that the reaction volume constituted by the set of tubes corresponding to the second half of the length of the cracking tube is 1.3 to 4 times greater than that corresponding to the first half of the length of the tube.
  • Figure 1 schematically illustrates a horizontal steam cracking furnace comprising a thermal radiation enclosure (1) through which passes a cracking tube arranged in the form of a coil consisting of eight horizontal straight sections connected together by elbows, the sections (2) and (3) having an internal diameter of 81 mm, the sections (4) and (5) an internal diameter of 99 mm, the sections (6) and (7) an internal diameter of 117 mm and the sections ( 8) and (9) an internal diameter of 135 mm, the inlet and outlet of the cracking tube in the thermal radiation enclosure being respectively in (10) and (11).
  • the steam cracking furnace comprises a thermal radiation enclosure provided with heating means constituted by burners, arranged for example in rows on the floor and / or on the walls of the enclosure.
  • the arrangement, adjustment and / or size of the burners in the thermal enclosure are such that the thermal power decreases along the cracking tube from the inlet to the outlet of the enclosure.
  • the ratio between the thermal power of the burners applied to the first half of the length of the cracking tube, located towards the inlet of the enclosure, and that applied to the second half of the length of the tube, located towards the output of this enclosure is between 60/40 and 85/15, preferably between 67/33 and 80/20, and in particular between 67/33 and 75/25.
  • This decreasing profile of the thermal power of the burners applied along the cracking tube can be easily obtained, by appropriately adjusting the gas or fuel-gas supply rate of each of the burners.
  • Another way is to have burners of the appropriate size and heating capacity in the thermal enclosure.
  • the maximum heating power must be such that the skin temperature does not exceed the limit compatible with the nature of the metal or alloy constituting the cracking tube.
  • a steam cracking furnace as shown diagrammatically in FIG. 1, comprises a thermal radiation enclosure (1) in briquetting constituted by a rectangular parallelepiped whose internal dimensions are 9.75 m for the length, 1.70 m for width and 4.85 m for height.
  • This cracking tube is arranged in the form of a serpentine, comprising eight horizontal straight sections, of equal length each, connected to each other by elbows.
  • the internal diameter of the sections (2) and (3) located towards the entrance to the thermal enclosure is 81 mm; the following sections (4) and (5) have an internal diameter of 99 mm; then the sections (6) and (7) have an internal diameter of 117 mm; the internal diameter of the sections (8) and (9) located towards the outlet of the thermal enclosure is 135 mm.
  • the internal diameters of the cracking tube at the inlet (10) and at the outlet (11) of the enclosure (1) being 81 mm and 135 mm respectively, the ratio between the internal diameters of the tube to the exit and entry is therefore 1.7.
  • the reaction volume of the second half of the length of the cracking tube, corresponding to the straight sections (6), (7), (8), (9), is 1.95 times greater than the reaction volume of the first half the length of the cracking tube, corresponding to the straight sections (2), (3), (4) and (5).
  • the thermal flux table measured inside the thermal radiation enclosure of the furnace is, under these conditions, represented in FIG. 3 by the surface inscribed in the three-dimensional graph connecting by the three coordinate axes, the length L of the thermal enclosure, the height H of this enclosure and the thermal flux F.
  • FIG. 3 shows, in particular, that the maximum of the thermal flux of radiation is located in the upper part of the thermal enclosure, corresponding to the first half the length of the cracking tube located towards the entrance to the thermal radiation enclosure.
  • a mixture of ethane and water vapor is circulated.
  • the composition of the mixture of ethane and water vapor used is such that the weight ratio of the amount of ethane to the amount of water vapor is 2.25.
  • Ethane is thus introduced into the cracking tube at a rate of 1800 kg / h and water vapor at a rate of 800 kg / h.
  • the cracking temperature of the mixture of ethane and water vapor rises from 695 ° C at the entrance to the radiation zone of the furnace up to 848 ° C at the exit from this zone.
  • the pressure of the mixture is at the outlet of the oven of 170 kPa.
  • the average residence time of the mixture of ethane and water vapor circulating in the cracking tube between the inlet and the outlet of the radiation zone of the furnace is 530 milliseconds.
  • a steam cracking oven comprises a thermal radiation enclosure, identical in shape and size to that of Example 1.
  • a cracking tube of refractory steel based on nickel and chromium, of a weight is placed. total substantially identical to that of Example 1, having an internal diameter of 108 mm, a thickness of 8 mm and, taking into account the capacity of the enclosure and the thermal constraints of the oven, a total length of 80 meters between the entrance and exit of the enclosure.
  • This cracking tube is arranged in the form of a coil comprising eight straight horizontal sections, of equal length each, connected to each other by elbows. The internal diameter of these straight sections is constant and equal to 108 mm.
  • the reaction volume of the first half of the length of the cracking tube, corresponding to the first four straight sections is identical to the reaction volume of the second half of the length of the cracking tube, corresponding to the last four straight sections.
  • the thermal radiation enclosure of the steam cracking furnace is provided with burners arranged on the walls of the enclosure, in five horizontal rows, located at equal distance from each other. The thermal power of all of these burners is evenly distributed between these five rows. Thus, the ratio between the thermal power of the burners applied to the first half and that applied to the second half of the length of the cracking tube is 50/50.
  • the thermal flux table measured inside the thermal radiation enclosure of the furnace is, under these conditions, represented in FIG. 4 by the surface inscribed in the three-dimensional graph connecting by the three coordinate axes, the length L of the thermal enclosure, the height H of this enclosure and the thermal flux F.
  • FIG. 4 shows, in particular, that the maximum of the thermal flux of radiation is located in the relatively central zone of the thermal enclosure.
  • a mixture of ethane and water vapor is circulated, identical to that used in Example 1.
  • the ethane is introduced therein at a rate of 1800 kg / h and the vapor water at a flow rate of 800 kg / h.
  • the cracking temperature of the mixture of ethane and water vapor rises from 640 ° C at the entrance to the oven radiation zone up to 848 ° C at the exit from this zone.
  • the pressure of the mixture is at the outlet of the oven of 170 kPa. Given the distribution of the heat flux in the enclosure, the thermal power applied to the second half of the length of the cracking tube is identical to that applied to the first half of the length of the tube.
  • the average residence time of the mixture of ethane and water vapor circulating in the cracking tube between the inlet and the outlet of the radiation zone of the furnace is 580 milliseconds.
  • Example 2 The operation is carried out in a steam cracking furnace identical to that of Example 1.
  • a mixture consisting of gaseous hydrocarbons comprising 64% by weight of n-butane, 25% by weight of is circulated in the cracking tube of this furnace.
  • isobutane 10% by weight of butene-1 and 1% by weight of isobutene, and water vapor.
  • the composition of this mixture of gaseous hydrocarbons and water vapor used is such that the weight ratio of the quantity of gaseous hydrocarbons to that of water vapor is 2.3.
  • the gaseous hydrocarbons and the water vapor are thus introduced into the cracking tube at flow rates of 2300 kg / h and 1000 kg / h respectively.
  • the cracking temperature of this mixture rises ve from 620 ° C at the entrance to the oven radiation zone up to 836 ° C at the exit from this zone.
  • the pressure of this mixture is at the outlet of the oven of 185 kPa.
  • the thermal power applied to the first half of the length of the cracking tube is 3.1 times greater, as in Example 1, than that applied to the second half of the length of the tube.
  • the average residence time of this mixture circulating in the cracking tube is 580 milliseconds between entering and leaving the radiation zone of the furnace.
  • Example 3 The operation is carried out in a steam cracking oven identical to that of Example 2. A mixture identical to that used in Example 3 is circulated in the cracking tube of this oven and at flow rates also identical to those of l 'example 3.
  • the cracking temperature of this mixture rises from 580 ° C at the entrance to the oven radiation zone up to 836 ° C at the exit from this zone.
  • the pressure of this mixture is at the outlet of the oven of 185 kPa.
  • the thermal power applied to the first half of the length of the cracking tube is identical, as in Example 2, to that applied to the second half of the length of the tube.
  • the average residence time of this mixture circulating in the cracking tube is 635 milliseconds between entering and leaving the radiation zone of the furnace.
  • a vertical-type steam cracking oven comprises a thermal brick radiation enclosure made up of a rectangular parallelepiped whose internal dimensions are 9.75 m for length, 1.60 m for width and 9.60 m for the height.
  • a cracking tube of refractory steel based on nickel and chromium having an average internal diameter of 98.5 mm, a thickness of 8 mm and, taking into account the capacity of the enclosure, is placed. a total length of 64 meters. The ratio between the length and the mean internal diameter is 650.
  • This cracking tube is arranged in the form of a coil, comprising eight vertical straight sections, of equal length each, connected to each other by elbows.
  • the internal diameter of the first two sections located towards the entrance to the thermal enclosure is 76 mm; the following two sections have an internal diameter of 84 mm; the next two sections have an internal diameter of 104 mm; and finally the internal diameter of the last two sections located towards the exit of the thermal enclosure is 130 mm.
  • the internal diameters of the cracking tube at the inlet and at the outlet of the thermal radiation enclosure being 76 mm and 130 mm respectively, the ratio of the internal diameters of the tube at the outlet and at the inlet is therefore 1.7.
  • the reaction volume of the second half of the length of the cracking tube, corresponding to the first four straight sections is 2.16 times greater than the reaction volume of the first half of the length of the cracking tube, corresponding to the last four. straight sections.
  • the thermal radiation enclosure of the steam cracking furnace is provided with burners arranged on the walls of the enclosure, in five vertical rows, located at equal distance from each other.
  • the thermal power of the burners is distributed along the cracking tube, so that the first half of the length of the tube, corresponding to the first four straight sections, receives 70% of the total thermal power, while the second half of the length of the tube, corresponding to the last four straight sections, receives 30% of the total thermal power.
  • the liquid hydrocarbons consist of a naphtha of density 0.684, having a distillation range ASTM 45/185 ° C and weight contents of 38.2% in linear paraffins, of 36.9% in branched paraffins, of 17.1% in cyclic compounds and 7.8% in aromatic compounds.
  • the composition of the mixture of naphtha and water vapor used is such that the weight ratio of the quantity of naphtha to the quantity of water vapor is 2.1.
  • the cracking temperature of the mixture of naphtha and water vapor rises from 600 ° C at the entrance to the radiation zone of the furnace up to 846 ° C at the exit from this zone.
  • the evolution of the cracking temperature of the mixture along the cracking tube is described by the curve (a) of FIG. 2 representing on the abscissa the average residence time (in milliseconds) of the mixture circulating in the cracking tube from l 'entry to the exit of the radiation area of the oven and on the ordinate the cracking temperature (in ° C) of the mixture.
  • Curve (a) shows that the cracking temperature of the mixture increases in its initial part relatively rapidly as a function of the average residence time.
  • the maximum skin temperature along the cracking tube is 1000 ° C.
  • the pressure of the mixture leaving the oven is 170 kPa.
  • the thermal power applied to the first half of the length of the cracking tube, located towards the entrance to the radiation zone is 2.3 times greater than that applied to the second half of the length of the tube, located towards the exit of this zone.
  • the average residence time of the mixture of naphtha and water vapor circulating in the craqua tube is 560 milliseconds.
  • a vertical type steam cracking oven comprises a thermal radiation enclosure identical in shape and size to that of Example 5.
  • a cracking tube of refractory steel based on nickel and chromium having a internal diameter of 98.5 mm, a thickness of 8 mm and a total length of 64 meters between the entrance and the exit of the enclosure.
  • the ratio between the length and the internal diameter of the tube is 650.
  • This cracking tube is arranged in the form of a coil comprising eight straight vertical sections, of equal length each, connected to each other by elbows.
  • the internal diameter of these straight sections is constant and equal to 98.5 mm.
  • the reaction volume of the first half of the length of the cracking tube, corresponding to the first four straight sections is identical to the reaction volume of the second half of the length of the cracking tube, corresponding to the last four straight sections.
  • the thermal radiation enclosure of the steam cracking furnace is fitted with burners arranged on the walls of the enclosure.
  • the thermal power of all of these burners is distributed homogeneously along the cracking tube, so that the ratio between the thermal power of the burners applied to the first half and that applied to the second half of the length of the cracking tube is 50/50.
  • a mixture of naphtha and water vapor is circulated, identical to that used in Example 5.
  • the naphtha is introduced therein at a rate of 2100 kg / h and the vapor of water at a flow rate of 1000 kg / h.
  • the cracking temperature of the mixture of naphtha and steam rises from 560 ° C at the entrance to the radiation zone of the furnace up to 846 ° C at the exit from this zone.
  • the evolution of the cracking temperature of the mixture along the tube is described by curve (b) in FIG. 2.
  • Curve (b) shows that the cracking temperature of the mixture increases in its initial part relatively slowly as a function of the average residence time.
  • the maximum skin temperature along the cracking tube is 1020 ° C.
  • the pressure of the mixture leaving the oven is 170 kPa.
  • the average residence time of the mixture of naphtha and water vapor circulating in the cracking tube between the inlet and the outlet of the radiation zone of the furnace is 610 milliseconds.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
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  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP87108912A 1986-06-25 1987-06-22 Procédé et four de vapocraquage d'hydrocarbures destines à la fabrication d'oléfines et de dioléfines Expired - Lifetime EP0252356B1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
FR8609219 1986-06-25
FR8609221 1986-06-25
FR8609219A FR2600667B1 (fr) 1986-06-25 1986-06-25 Procede et four de vapocraquage d'hydrocarbures liquides destines a la fabrication d'olefines et de diolefines
FR8609221A FR2600642B1 (fr) 1986-06-25 1986-06-25 Procede et four de vapocraquage d'hydrocarbures gazeux pour la fabrication d'olefines et de diolefines

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EP0252356A1 EP0252356A1 (fr) 1988-01-13
EP0252356B1 true EP0252356B1 (fr) 1990-10-03

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EP87108912A Expired - Lifetime EP0252356B1 (fr) 1986-06-25 1987-06-22 Procédé et four de vapocraquage d'hydrocarbures destines à la fabrication d'oléfines et de dioléfines

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US (2) US4762958A (enrdf_load_stackoverflow)
EP (1) EP0252356B1 (enrdf_load_stackoverflow)
JP (1) JPS6366290A (enrdf_load_stackoverflow)
CA (1) CA1256124A (enrdf_load_stackoverflow)
DE (1) DE3765325D1 (enrdf_load_stackoverflow)
ES (1) ES2018665B3 (enrdf_load_stackoverflow)

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FR2631957B1 (fr) * 1988-05-30 1990-08-31 Bp Chimie Sa Procede et appareillage de fabrication d'olefines et de diolefines par reaction de vapocraquage d'hydrocarbures controlee a l'aide d'un systeme comprenant un spectrophotometre infrarouge
US5078857A (en) * 1988-09-13 1992-01-07 Melton M Shannon Delayed coking and heater therefor
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Also Published As

Publication number Publication date
EP0252356A1 (fr) 1988-01-13
JPH0556797B2 (enrdf_load_stackoverflow) 1993-08-20
US4997525A (en) 1991-03-05
JPS6366290A (ja) 1988-03-24
DE3765325D1 (de) 1990-11-08
US4762958A (en) 1988-08-09
ES2018665B3 (es) 1991-05-01
CA1256124A (en) 1989-06-20

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